RU2532743C2 - Method and device for capturing co2 - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: method includes the introduction of drops of an absorption liquid into a gas flow, mainly, in the direction of the gas flow, capturing CO₂ from the gas flow during a phase of capturing by means of the drops of the absorption liquid, with the drops of the absorption liquid being introduced into the gas flow at a high rate, sufficient for the provision of an internal circulation in a mass of a drop of the absorption liquid, and the drops of the absorption liquid being introduced into the gas flow with the Sauter mean diameter in the interval from 50 to 500 mcm. A device for capturing CO₂ is described.

EFFECT: reduction of capital expenditures and energy consumption.

19 cl, 7 dwg

Description

The present invention relates to an apparatus and method for collecting CO ₂ from an exhaust gas stream.

When fuel is burned, including coal, fuel oil, gas, waste, etc., a hot process gas (or off-gas) is generated at a combustion station, including a station connected to boiler devices to provide steam to the power station. Such exhaust gas often contains, among other substances, carbon dioxide (CO ₂ ). The negative environmental consequences of the release of carbon dioxide into the atmosphere are widely known, which led to the development of processes adapted to separate carbon dioxide from the hot process gas generated by the combustion of the above types of fuel.

The traditional way of separating CO ₂ from the exhaust gas is to use the standard absorption-desorption process, which is illustrated in FIG. In this process, the pressure of the exhaust gas is increased by means of a supercharger before or after the refrigerator with indirect or direct contact. Then the exhaust gas enters the absorption column, where it enters countercurrent contact with the absorbent moving down. A flushing section is installed at the top of the column to remove, mainly with water, residues of absorbent material following the exhaust gas from the CO ₂ separation section. The enriched CO ₂ absorbent from the lower part of the absorber is pumped to the upper part of the desorption column through a heat exchanger-heat exchanger, heating the enriched absorbent before entering the desorption column. In a desorption column, CO _{2 is} stripped with steam, which rises along the column. Water and absorbent that follow the CO ₂ in the upper part are separated in the condenser above the upper part of the stripper. Steam is generated in the reboiler, from which the CO ₂ depleted absorbent is pumped through the heat exchanger-utilizer and the refrigerator to the top of the absorption column.

Known methods for separating CO ₂ from the exhaust gas use equipment that causes a pressure drop in the exhaust gas. If such a pressure drop is allowed, this will lead to an increase in pressure at the outlet of the power plant or other station where the off-gas is generated. This is undesirable. In the case of a gas turbine, this can lead to a decrease in the efficiency of the power generation process. To overcome this drawback, an expensive exhaust gas blower is required.

A further problem of the existing technology is that the absorption tower and the preceding flue gas cooler are also expensive equipment.

Standard setting for capturing CO ₂ also requires a large space structures.

WO 00/74816 describes a device for collecting CO ₂ . This device can be installed as a horizontal channel in which the exhaust gas comes into contact with two different absorption liquids in two adjacent sections. A screen is provided that prevents the flow of fluid from one section to the next section. These liquids are regenerated and reused.

Bandyopadhyay et al. In the article, “Critical Flow Sprayer in the SO ₂ Jet Compartment” (Chemical Engineering Journal, 2008, 139, pp. 29-41) concluded that the SO ₂ separation efficiency increases with increasing fluid flow rate, the ratio of fluid and gas flow rates, atomizing air pressure and dripping speed. The same conclusion was reached by Srinivasan et al. In the article “Mass transfer to droplets formed during the controlled termination of cylindrical jet physical absorption” (Chemical Engineering Science, 1988, v. 43, No. 12, pp. 3141-3150 )

An object of the present invention is to provide a method and apparatus for separating CO ₂ from an off-gas stream, the method providing a reduced pressure drop, independent of the use of off-gas blowers, and preferably requires less energy than the conventional method. In addition, the goal is to propose a solution that has significantly less negative consequences. Another goal is to propose a solution that can be integrated with a new efficient desorption method and device.

The next goal is to offer a device and method that can be effectively combined with a facility using reuse.

In addition, the goal is to provide a device that can be used in combination with pre-treatment devices to separate other undesired compounds from the gas stream.

The above objectives are achieved by means of the device and method according to the independent claims. Additional useful features and embodiments are presented in the dependent claims.

The present invention relates to the capture of CO ₂ from the exhaust gas and is a so-called technology for processing combustion products. The present invention can be used in connection with gases leaving various devices. These devices can be gas-fired combined-cycle power plants, coal-fired power plants, boilers, cement plants, oil refineries, heating furnaces for endothermic processes, including steam reforming of natural gas or similar sources of off-gas containing CO ₂ .

A long off-gas channel will be required in almost all cases of CO ₂ capture from the off-gas to transport gas from the plant in which the gas is generated to the CO ₂ trap. Its implementation for effective use, essentially, will not require additional costs for the channel for the exhaust gas.

According to one aspect of the present invention, the necessary contact area between the gas and the liquid is provided by spraying liquid droplets into the gas in the exhaust gas channel itself, thereby eliminating the absorption column. A direct contact refrigerator (CFC), which usually precedes this column, can also be eliminated by providing the same contact in the section of the channel itself.

An object of the present invention is to use a portion of the off-gas channel, which is in any case necessary for transporting the off-gas to a CO ₂ trap. Usually a lot of space is required to make the installation for trapping CO ₂ in a built-in power. As a result of this, the traditional KNK and the absorption column are eliminated. This method provides a very significant reduction in costs.

It is assumed that the channel should be almost horizontal, but it can be at an angle from 0 ° to 60 °. The tilt can be directed in any direction, and the direction of the tilt can vary throughout the channel. The channel can also change direction once or repeatedly from 1 to 360 degrees.

The present invention reduces both capital costs and energy consumption.

According to one embodiment of the present invention, the nozzles direct the jet mainly in the direction of the exhaust gas stream, whereby the gas moves along the channel. The kinetic energy of the droplets thus transmitted to the gas overcomes the drop in gas pressure in the channel. This means that the upstream channels (channel) can be used with lower absolute pressure. As a result, the pressure at the outlet of the upstream gas turbine (when used) can be set at a lower level compared to standard technology, and such reduced pressure at the outlet of the gas turbine increases the efficiency of the gas turbine, leading to an increase in electricity production.

This method reduces capital costs, saves energy, and can even lead to an increase in electricity production in a gas turbine.

These and other goals are achieved by the method according to claim 1 and the device according to claim 6. Other advantages and useful embodiments are provided in the dependent claims.

The present invention will now be described in detail with reference to the accompanying drawings, in which:

figure 1 illustrates a traditional method of absorption-desorption;

FIG. 2 illustrates a flow chart of an embodiment of the present invention; FIG.

figure 3 illustrates an embodiment in which the channel includes a direct contact and flushing section;

FIG. 4 represents the lines of work and equilibrium for the CO ₂ absorption process of FIG. 3;

5 illustrates an embodiment with an integrated preprocessing section;

6 illustrates an embodiment with off-gas recirculation; and

Fig.7 is a cross section showing the relative speed of the internal circulation, developing in a drop of liquid when moving in a gas.

Figure 1 presents a traditional method for separating CO ₂ from the exhaust gas using a standard absorption-desorption process. In this process, the pressure of the exhaust gas P10 is increased by means of a supercharger P21 before (as illustrated in the drawing) or after the refrigerator with indirect or direct contact P20. The exhaust gas then enters the absorption tower P22, where it enters countercurrent contact with the absorbent P40 flowing downward. A flushing section is installed at the top of the column to separate, mainly with water, absorbent residues following the exhaust gas from the CO ₂ separation section. The washing liquid P41 flows into the upper part and then goes down in the form of P42. The CO ₂ depleted exhaust gas is discharged through the top as P12. The CO ₂ enriched absorbent P32 from the lower part of the absorber is pumped to the upper part of the P30 desorption column through a heat exchanger-utilizer P28, which heats the enriched absorbent P36 before entering the P30 desorption column. In a desorption column, CO _{2 is} stripped with steam, which moves up the column. Water and absorbent following CO ₂ from the upper part are separated in the condenser P33 above the upper part of the stripper. Steam is generated in the reboiler P31, from where the depleted CO ₂ absorbent P38 is pumped through the heat exchanger-heat exchanger P28 and the refrigerator P29 to the top of the absorption tower P22. The steam enters the reboiler as stream P61. The separated CO ₂ leaves as stream P14.

Figure 2 illustrates the main fluid flows in an embodiment of the present invention. Exhaust gas 10 enters the channel 1 from one end. An absorption liquid containing a CO ₂ absorbent and a diluent is sprayed into the channel through the nozzle 15. The absorption liquid is sprayed mainly in the direction of the exhaust gas flow at a high enough speed to at least compensate for the decrease in pressure in the first part of the channel. Drops of absorption liquid move through the exhaust gas stream and absorb the CO ₂ contained therein. The CO ₂ -based absorption liquid is collected upstream at a collection point 23 at the bottom of the channel. Drops are collected using a mist eliminator / droplet eliminator. Enriched CO ₂ absorbing liquid 19 is pumped via pump 34 into the conduit 32 connected to the stripping device. The desorption device may be a conventional desorption device, as illustrated in FIG. 1, or it may be any other device for desorption of CO ₂ from an absorption liquid. In the embodiment illustrated in FIG. 2, the exhaust gas continues to flow down the channel, and the second absorption liquid is sprayed into the gas through the nozzle 17. The absorption liquid is sprayed mainly in the direction of the exhaust gas flow and at a sufficiently high speed so that at least compensate for the decrease in pressure in this second part of the channel. Drops of absorption liquid move through the gas stream and absorb the CO ₂ contained in it. The CO ₂ -based absorption liquid is collected upstream at a collection point 24 at the bottom of the channel. The CO ₂ enriched absorption liquid collected at point 24 is pumped upwardly through the pump 16 to the nozzle 15. The exhaust gas continues to flow down the channel, and the depleted absorption liquid 40 is sprayed into the gas from the nozzle. The absorption liquid is sprayed mainly in the direction of the exhaust gas flow and at a high enough speed to at least compensate for the decrease in pressure in this third part of the channel. Drops of absorption liquid move through the exhaust gas stream and absorb the CO ₂ contained therein. Enriched with CO ₂ absorption liquid is collected in the upstream collection point 25 at the bottom of the channel. Enriched with CO ₂ absorption liquid collected at the point 25, is pumped upwardly through the pump 18 to the nozzle 17. The CO ₂ depleted exhaust gas exits the channel at the other end as stream 12.

The channel can be horizontal or inclined at an angle of up to 60 degrees. The channel may further include one or more mist eliminators or similar means for collecting droplets of absorption liquid. Then these droplets are introduced at a sufficiently high speed to propel the gas flow forward through the mist eliminators.

Figure 2 illustrates the main configuration of the processing in the transverse flow in the channel for the exhaust gas. The nozzles in this drawing are directed downward. This is done, however, only for the convenience of drawing. It is envisaged that the nozzles are directed mainly in the direction of the gas flow, but other configurations are possible, in which, for example, the nozzles form a row or a bundle and are directed in different directions. Additional examples may be given.

One embodiment of the present invention can be described with reference to FIG. The off-gas enters the off-gas channel, which typically does not contain processing equipment for 150-250 meters and which leads to a traditional CO ₂ trap. At a convenient point, a short distance from the exhaust gas inlet, in section C, cold water is sprayed, creating cooling by direct contact. Cooling water recirculates with the exception of possible purification. Recirculation is carried out through the pump and the refrigerator to the point at which this stream is mixed with the compressed gas in the spray nozzles (nozzles). The droplets formed in this section are collected downstream in droplet eliminators.

In another embodiment, the pressure of the cooling water is increased to 5-100 bar (0.5-10 MPa), preferably 5-10 bar (0.5-1 MPa), by a pump, before the water exits through the spray nozzles. The absorption liquid can also be introduced into the channel in the same way.

The gas for spraying through the nozzles is compressed in the compressor, common to all nozzle batteries in which the nozzles are used. In one embodiment, the suction gas is exhaust gas, appropriately separated from the channel after the drip eliminators of the CNS section.

Then, the cooled off-gas enters the absorption section of CO ₂ A1, where it comes into contact in a parallel and perpendicular flow with the most enriched CO ₂ absorbent solution passing through the absorption process. The liquid is again sprayed into the channel through the nozzles. Drops of liquid are captured downstream in droplet eliminators. The collected enriched absorption liquid is pumped from section A1 to a desorption process, which is not described in detail here. The liquid absorbent that is sprayed in section A1 is pumped from section A2, where the CO ₂ content in the exhaust gas is reduced and thus the liquid at the outlet is less enriched in CO ₂ than the liquid at the outlet from section A1. The lines of work and equilibrium for the process of separation of CO ₂ presented in figure 4. In addition, section A2 provides the contact of gas and liquid in accordance with the same mode as in section A1. The liquid in section A2 comes from section A3, where the levels of CO ₂ are minimal in both phases, including in the exhaust gas and in the liquid. The absorption liquid sprayed into section A3 is a depleted absorbent that is returned from the desorption process in a regenerated state. Drip eliminators installed downstream of section A3 must be appropriately designed to provide stiffer catching of droplets than other sections because any reduction in absorbent material leads to higher requirements for the regeneration section of absorbent W.

The function of the section is to wash almost all the absorbent that is carried out with gas from section A3. This is achieved by circulating mainly water in the entire section through a pump and a refrigerator. The nozzle for recirculating the captured absorbent stream and wash water is conveniently used in the recirculation stream. The potential for separating the absorbent from the exhaust gas is determined by the concentration of free absorbent in the wash liquid and its temperature. This may require more than one such washing section, and it can be easily supplemented.

It has been found that spray droplets propel the gas along the channel to such an extent that no exhaust gas blower is required.

The number of stages required for the absorption of CO ₂ is in a ratio of compromise with the flow of absorbent. In principle, one stage would be sufficient if a sufficient amount of liquid circulated, but this would require a lot of liquid. The possible number of stages is two or more. For a standard countercurrent absorption column, it can be shown that two or three equilibrium steps would be sufficient.

According to one embodiment, the present invention can be combined with a pretreatment and waste gas reuse section. These features are described in more detail in FIGS. 5 and 6.

Figure 5 presents one embodiment of the present invention, supplemented by pre-treatment of the exhaust gas. This is appropriate for coal-fired power plants and a variety of industrial plants where CO ₂ separation is required. Pre-processing may perform one or more functions. It can, for example, be a wash with sea water, where the buffering properties of sea water are used to absorb SO ₂ from the off-gas. If this were not the case, SO ₂ would react irreversibly with the alkaline absorbent used to capture CO ₂ , as a result of which its consumption would increase. In this way, the exhaust gas can also be cleaned of particles. Both of these functions are usually required after the coal combustion process. The flue gas from the aluminum smelter may contain HF, and more examples can be given. The regeneration of the fluid in the pre-treatment section can, for example, be carried out using a particle trapping filter. In the case of absorption of SO ₂ in seawater, the best mode of action is to install a nozzle into which SO ₂ is piped with seawater in the form of sulfite, which, in turn, is oxidized in seawater to sulfate, and this substance is already abundant in sea water.

In the pre-treatment section, you can use the same technologies for the nozzle and droplet eliminator as in other sections.

FIG. 6 illustrates one embodiment of the present invention, which includes a pre-treatment section coupled to exhaust gas recirculation (EGR). The advantage of using EGR is that the off-gas volumetric flow is significantly reduced, thereby allowing a reduction in cross-sectional area in the gas flow sections and a higher CO ₂ content in the off-gas, which reduces processing capital costs.

7 is a cross section showing the relative speed in the internal circulation mode, developing in a drop of liquid moving in a gas. The gas moves in the horizontal direction and leads to a toroidal (donut-shaped) flow, which is known as the Hill Vortex. The reason for the internal circulation is the shear force on the surface of the liquid droplet, which is created by the movement of the gas along the surface. It is known that a drop of liquid that moves through a viscous fluid, such as a CO ₂ gas stream, tends to circulate internally due to shear stress applied to its interface between the surrounding fluid. Heat transfer and mass transfer sharply increase with a decrease in the thickness of the boundary layer. Compared to the so-called hard drop (i.e., a liquid drop with zero or very little internal circulation), the transfer coefficients for a liquid drop with internal circulation are at least 2-4 times larger.

According to a useful embodiment of the present invention, an absorption liquid, for example an amine, is introduced or sprayed into the channel 1 using nozzles 15, 17, 40. The exhaust gas 10, including a gas stream that contains CO ₂ , moves through the channel 1 with a speed of component 5 up to 15 m / s. The diameter of the exhaust gas channel 1 may depend on the amount of exhaust gas emitted by a power plant, cement plant or similar production, but in most cases it is from 3 to 10 meters. The flow conditions in the exhaust gas channel will thus be highly turbulent with a Reynolds number well above 100,000.

The absorption liquid exits one or more nozzles 15, 17, 40 in the form of small drops at a speed of 30-120 m / s. It is assumed that the droplets will be turbulent for a short time (1-2 seconds) after they exit the nozzle. The relative difference in the velocities of the droplets of the absorption liquid and the exhaust gas causes a high shear stress on the droplets, which helps to maintain internal circulation inside the droplet and, possibly, preserves the turbulence conditions inside the droplet. Therefore, the mass transfer in the area near the nozzles will be extremely high.

The main disadvantage of the absorber with the nozzle is the ability to mass transfer CO ₂ (gas) to CO ₂ (water). The mass transfer rate depends on the thickness of the gas film and the corresponding diffusion. They, in turn, depend on the flow rates. In absorbers with a nozzle, a laminar flow is carried out, which leads to a significantly lower mass transfer of CO ₂ (gas) to CO ₂ (water) in comparison with the turbulent flow conditions. High turbulence in channel 1 and turbulence / internal circulation in the droplets leads to a significantly reduced resistance to mass transfer. Unlike traditional methods for absorbing CO ₂ from the off-gas 10, the transfer of CO ₂ from the off-gas 10 to droplets of absorption liquid will be significantly higher due to a decrease in the film thickness, and the transfer of CO ₂ (water) does not depend on diffusion, but on convection. Thus, the reaction with the absorbent will be much faster.

The size of the droplets of the absorption liquid may change when the pressure on the absorption liquid in front of the nozzle or nozzles changes, or when the flow rate of the droplets of the absorption liquid through the nozzle or nozzles changes. The size and shape of the nozzle or nozzles will also affect the size of the droplets of the absorption liquid. The relative difference between the average gas flow rate and the average droplet velocity of the absorption liquid will also affect the droplet size. If the ratio of the average gas flow rate to the average droplet speed of the absorption liquid during the exit of the absorption liquid from the means for introducing the absorption liquid is more than about 3, preferably from 6 to 10, this will help to ensure internal circulation in the drops of absorption liquid introduced into the containing CO ₂ gas flow, and the fact that the average diameter of the droplets of the absorption liquid according to Sauter will remain relatively small, preferably of the order of 50-500 microns.

Also, the residence or droplet time of the droplets of the absorption liquid through the channel 1 is important. When the droplets of the absorption liquid move through the channel for the exhaust gas, the initial collisions between the drops and the exhaust gas will facilitate further grinding of the droplets. At the same time, the force / shear stress acting on the droplets will help maintain internal circulation within the droplet. In this initial phase of the passage of a drop of absorption liquid, the mass transfer of CO ₂ from the exhaust gas and into the drops of absorption liquid reaches a maximum level. When droplets of absorption liquid move along channel 1, their speed decreases due to numerous collisions and braking forces (kinetic energy is transferred from the droplet to the exhaust gas). In addition, the size of the droplets of the absorption liquid can also increase due to coalescence, which further reduces their speed and leads to a decrease in the area of the active surface of the liquid. The saturation of the droplets of the absorption liquid also begins as a result of the reaction with CO ₂ (water). As a result of this, the mass transfer of CO ₂ from the exhaust gas and into the drops of the absorption liquid begins to decrease. This period between the introduction of droplets of absorption liquid into the channel 1 and a significant reduction in the mass transfer of CO ₂ from the exhaust gas determines the desired residence time or passage of droplets of absorption liquid in the gas stream and, thus, also helps determine the preferred length of the channel 1 before collecting the absorption liquid, for example, using droplet eliminators. In this regard, it can be understood that any obstacles in the channel, for example, the material of the filler of the absorber nozzle, etc., will only reduce the residence time or flight time, and this, therefore, will prevent the mass transfer of CO ₂ from the exhaust gas and into the drops of the absorption liquid . In addition, any obstructions in the channel, such as filler material, etc., may increase the pressure loss along the channel, which should preferably be avoided.

According to the present invention, CO ₂ absorption occurs when drops of the absorption liquid are carried through the air, i.e. are suspended in a gas stream containing CO ₂ . It is also called the term “capture phase". The capture phase occurs in the capture zone. The capture zone can be defined as the region or volume between the means for introducing the absorption liquid and the collection point of the absorption liquid located downstream of the means for introducing the absorption liquid. According to the present invention, it is preferable that no obstacles, such as filler materials or other surfaces that can cause the absorption liquid to collect inside or on the surface of the obstacles, are not present in this capture zone or during the capture phase. A major advantage of the present invention is that CO _{2 is} transferred from the gas stream to the absorption liquid when the absorption liquid is carried through the air or suspended in a gas stream. However, it is possible to envisage a next CO ₂ capture step involving an absorber nozzle or some other capture device after the capture zone according to the present invention. For example, an assembly means 23 for collecting saturated CO ₂ droplets of absorption liquid installed downstream of the means for introducing absorption liquid 15, 17, 40 may include, in particular, an absorber nozzle or some other trapping device.

According to one embodiment of the present invention, the temperature of the absorption liquid introduced into the gas stream is in the range of 20 ° C to 80 ° C, preferably in the range of 20 ° C to 50 ° C. However, this depends on the type of absorption liquid used, and it is understood that other absorption liquids can be used at different temperature ranges.

It is clear that the advantages of the present invention can be used even when changing various technological parameters. Parameters that affect the mass transfer of CO ₂ from the exhaust gas and into the droplets of the absorption liquid include the following:

- channel diameter

- channel shape

- channel length

- time of stay or passage of drops of absorption liquid

- channel surface

- number of nozzles

- location of nozzles

- shape and design of nozzles

- pressure drops of the absorption liquid before exiting the nozzles

- flow rate of droplets of absorption liquid through nozzles

- exhaust gas velocity

- the rate of drops of absorption liquid

- the ratio of the velocities of the exhaust gas and drops of absorption liquid

- temperature drops of the absorption liquid

- flue gas temperature

- concentration of CO ₂ in the exhaust gas

- exhaust gas flow rate

- concentration of absorption liquid

- viscosity of the absorption liquid

etc.

After reviewing the present description, a specialist in the art will be able to evaluate the beneficial effects of the present invention, which are set forth in the following claims, provided that the above parameters are set in such a way that:

- CO _{2 is} captured from the gas stream during the capture phase by droplets of absorption liquid, where drops of absorption liquid are carried through the air during the capture phase;

- drops of absorption liquid are introduced into the gas stream at a high enough speed to provide internal circulation inside the drop of absorption liquid, and

- drops of absorption liquid are introduced into the gas stream with an average Sauter diameter in the range from 50 μm to 500 μm.

Claims (19)

1. A method for collecting CO ₂ from a gas stream, comprising introducing droplets of absorption liquid into the gas stream, mainly in the direction of the gas stream, characterized in that it involves collecting CO ₂ from the gas stream during the capture phase by droplets of absorption liquid, the absorption liquid is sprayed in the air during the capture phase, and the introduction of drops of absorption liquid into the gas stream at a rate sufficient to ensure internal circulation inside the drop of absorption liquid, while the average diameter o Sauter drops of absorption liquid introduced into the gas stream is in the range from 50 μm to 500 μm. 2. The method according to claim 1, in which the ratio between the average gas flow rate and the average droplet speed of the absorption liquid when it leaves the means for introducing the absorption liquid is more than 3, preferably in the range from 6 to 10. 3. The method according to any one of claims 1 or 2, in which the temperature of the absorption liquid introduced into the gas stream is in the range from 20 ° C to 80 ° C, preferably in the range from 20 ° C to 50 ° C. 4. The method according to any one of claims 1 or 2, in which the flow rate of the gas containing CO ₂ is from 5 to 15 m / s and the droplet speed of the absorption liquid is from 30 to 120 m / s, wherein the gas flow rate and velocity drops of absorption liquid are mainly parallel. 5. The method according to claim 1, wherein the CO ₂ enriched drops of absorption liquid are collected downstream of the means for introducing the absorption liquid. 6. The method according to claim 1, in which droplets of absorption liquid are introduced at a speed sufficient to move the gas stream during the CO ₂ capture phase without using additional equipment to compress the gas stream. 7. The method according to claim 6, in which there are no intervals between the means for introducing the absorption liquid and collecting saturated CO ₂ drops of the absorption liquid. 8. The method according to any one of claims 1, 2 or 5-7, wherein the CO ₂ -containing gas stream is highly turbulent. 9. A device for capturing CO ₂ from a gas stream, comprising means (15, 17, 40) for introducing absorption liquid, intended for introducing drops of absorption liquid, mainly in the direction of the CO ₂ containing gas stream (10), characterized in that has a capture zone in which drops of the absorption liquid trap CO ₂ from the gas stream (10), and drops of the absorption liquid are sprayed in the air throughout the capture zone, while it is configured to introduce drops of absorption liquid at a speed sufficient to provide the course of internal circulation inside the drops of absorption liquid and the production of drops of absorption liquid with an average Sauter diameter in the range from 50 μm to 500 μm. 10. The device according to claim 9, in which depleted drops of absorption liquid are introduced into the CO ₂ -containing gas stream (10) at a speed of 30-120 m / s. 11. The device according to claim 10, in which the speed of the CO ₂ -containing gas stream (10) is from 5 to 15 m / s. 12. The device according to claim 9, which contains a collection tool (23) for collecting saturated CO ₂ drops of absorption liquid downstream of the means (15, 17, 40) for introducing the absorption liquid and the capture zone. 13. The device according to claim 9, in which the means (15, 17, 40) for introducing the absorption liquid are configured to introduce droplets of the absorption liquid at a speed sufficient to move the gas stream through the device without using additional equipment for compressing the gas stream (10) . 14. The device according to item 13, in which the means (15, 17, 40) for introducing the absorption liquid and the collection tool (23) for collecting saturated CO ₂ drops of the absorption liquid are placed without intervals. 15. The device according to claims 9-14, which has a channel (1) for conducting a CO ₂ -containing gas stream (10), wherein means (15, 17, 40) are provided in the channel (1) for introducing the absorption liquid and a collection means ( 23) for collecting drops of absorption liquid downstream of the means (15, 17, 40) for introducing the absorption liquid, the channel (1) forming a trapping zone between the means (15, 17, 40) for introducing the absorption liquid and the collection means ( 23) to collect drops of absorption liquid. 16. The device according to claims 9-14, wherein the gas stream (10) is highly turbulent. 17. The device according to claims 9-14, in which the ratio between the average velocity of the CO ₂ -containing gas stream and the average droplet rate of the absorption liquid when the absorption liquid leaves the means for introducing the absorption liquid is more than 3, preferably in the range from 6 to 10. 18. The device according to claims 9-14, wherein the means (15, 17, 40) for introducing the absorption liquid include a nozzle or nozzles. 19. The device according to claims 9-14, wherein the collection means (23) for collecting drops of the absorption liquid includes a droplet eliminator and / or a mist eliminator.

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